System and method for integrated adsorptive gas separation of combustion gases

ABSTRACT

An integrated fuel combustion system with adsorptive gas separation separates a portion of carbon dioxide from a combustion gas mixture and provides for recycle of separated carbon dioxide to the intake of the fuel combustor for combustion. A process for carbon dioxide separation and recycle includes: admitting combustion gas to an adsorptive gas separation system contactor containing adsorbent material; adsorbing a portion of carbon dioxide; recovering a first product gas depleted in carbon dioxide for release or use; desorbing carbon dioxide from the adsorbent material and recovering a desorbed second product gas enriched in carbon dioxide for sequestration or use; admitting a conditioning fluid into the contactor and desorbing a second portion of carbon dioxide to recover a carbon dioxide enriched conditioning stream; and recycling a portion of the carbon dioxide enriched conditioning stream to an inlet of fuel combustor to pass through the fuel combustor for combustion.

1. RELATED APPLICATIONS

The present application claims the benefit of U.S. Pat. No. 9,146,036,filed Dec. 21, 2013 and entitled “System and Method for IntegratedAdsorptive Gas Separation of Combustion Gases”; and claims benefit ofPCT International Patent Application No. PCT/CA20120/050451, filed Jun.29, 2012 and entitled “System and Method for Integrated Adsorptive GasSeparation of Combustion Gases”; and claims benefit of U.S. ProvisionalPatent Application Ser. No. 61/504,197 filed Jul. 2, 2011 and entitled“System and Method for Integrated Adsorptive Gas Separation ofCombustion Gases”; the contents of each of which are herein incorporatedby reference in their entirety for all purposes.

The present invention is related to previously filed PCT InternationalPatent Application No. PCT/CA2011/050521, filed Aug. 26, 2011 andentitled “Method of Adsorptive Gas Separation using Thermally ConductiveContactor Structure”, the contents of which are herein incorporated byreference in their entirety. The present application is also related topreviously filed PCT International Patent Application No.PCT/CA2010/000251, filed Feb. 26, 2010 and entitled “Parallel PassageFluid Contactor Structure”, the contents of which are also hereinincorporated by reference in their entirety.

2. TECHNICAL FIELD

The present invention relates generally to methods for integratedadsorptive gas separation of combustion gases and systems therefore.More particularly, the present invention relates to methods ofintegrated adsorptive gas separation of combustion gases and recycle ofseparated combustion gases to a combustion process and systemsincorporating the same.

3. BACKGROUND OF THE INVENTION

Temperature swing adsorption methods are known in the art for use inadsorptive separation of multi-component gas mixtures. Many conventionaltemperature swing adsorption processes are used for preferentiallyadsorbing one component of a feed gas mixture on an adsorbent materialto separate it from the remaining feed gas components, and thensubsequently to regenerate the adsorbent material to desorb the adsorbedcomponent and allow for cyclic reuse of the adsorbent material. However,conventional temperature swing adsorption methods are typically limitedin their efficiency due in part to limitations in the desorption orregeneration of the adsorbent material used in an adsorptive separationsystem, and also to limitations in the adsorption phase of thetemperature swing adsorption process. Such inefficiencies inconventional temperature swing adsorption systems and methods have alsoled to inefficiencies in the integration of such systems into industrialsystems where separation of gas mixtures may be desired, leading toundesirable costs in capital, energy and/or operating efficiency.

One type of industrial process where gas separation may be desirableincludes combustion processes, where the separation of one or more gascomponent from a combustion process flue gas is required, such as forthe removal and/or sequestration of carbon dioxide gas from fossil fuelcombustion process flue gas mixtures, for example. In such applications,inefficiencies in conventional temperature swing adsorptive gasseparation systems have typically led to undesireably inefficientintegration of such temperature swing adsorptive gas separation systemsinto fossil fuel combustion processes, resulting in unacceptably highcapital costs, reductions in energy efficiency and/or efficiency of gasseparation, and operating costs, for example.

One inefficiency of typical conventional temperature adsorptionprocesses in fossil fuel combustion applications is the inefficientadsorption of a desired combustion gas component on the adsorbentmaterial, which may result from the rapid increase in temperature of theadsorption front when moving through the adsorbent material due to theheat of adsorption released as the gas component is adsorbed. In manyconventional temperature swing adsorption methods, such increases in thetemperature of the adsorbent material during adsorption may result indecreased adsorbent capacity associated with “hot spots” in theadsorbent material and a corresponding decrease in efficiency of thetemperature swing adsorption process. Another shortcoming of typicallyconventional temperatures swing adsorption methods in fossil fuelcombustion applications is the inefficient desorption or regeneration ofthe adsorbent material, which may result from the difficulty inuniformly heating the adsorbent material as thermal energy is requiredto meet the heat of desorption of the adsorbed compound duringdesorption or regeneration. Such non-uniformities in the heating of theadsorbent material may typically result in retained adsorption of a gascomponent associated with “cold spots” in the adsorbent material, or mayrequire the application of an unnecessarily large thermal flux tosufficiently desorb the gas component, which may lead to undesirablyhigh heating costs and leave the adsorbent material unnecessarilyoverheated following desorption, which undesirably affects continuedadsorption system performance, and may typically require additionaloperating cost intensive remedies such as additional cooling steps inorder to retain adsorptive functionality.

4. SUMMARY OF THE INVENTION

It is an object of the present invention to provide a method ofintegrated adsorptive gas separation for combustion gases that addressessome of the limitations of the prior art.

It is a further object of the invention to provide a method ofintegrated adsorptive gas separation for combustion gases using aparallel passage thermal swing adsorption (TSA) system integrated withina fossil fuel combustion system according to the present invention thataddresses some of the limitations of the prior art.

It is an object of the invention to provide an integrated adsorptive gasseparation for combustion gases using a parallel passage partialpressure swing adsorption (PPSA) system integrated within a fossil fuelcombustion system according to the present invention that addresses someof the limitations of the prior art.

It is a further object of the invention to provide an integratedadsorptive gas separation for combustion gases using a parallel passagepressure swing adsorption (PSA) system integrated within a fossil fuelcombustion system according to the present invention that addresses someof the limitations of the prior art.

It is yet a further object of the invention to provide an integratedfossil fuel combustion system including a TSA gas separation process forseparating carbon dioxide from a combustion gas mixture according to thepresent invention that addresses some of the limitations of the priorart.

In one aspect, an integrated adsorptive gas separation process forseparating at least a portion of a combustion gas mixture from a fuelcombustor is provided according to an embodiment of the presentinvention, wherein said combustion gas mixture comprises at least afirst component comprising carbon dioxide and a second component, theprocess comprising:

admitting said combustion gas mixture into an adsorptive gas separationsystem comprising at least one adsorbent material;

adsorbing at least a portion of said first component on at least onesaid adsorbent material;

recovering a first product gas depleted in said first component relativeto said combustion gas mixture from an outlet end of said adsorbentcontactor;

desorbing a first portion of said first component adsorbed on at leastone said adsorbent material;

recovering a desorbed second product gas enriched in said firstcomponent from at least one of said inlet and outlet ends of saidadsorptive gas separation system;

admitting a conditioning fluid into said adsorptive gas separationsystem and desorbing a second portion of said first component adsorbedon at least one said adsorbent material to recover a first componentenriched conditioning stream; and

recycling at least a portion of said first component enrichedconditioning stream recovered from said adsorptive gas separation systemto an air inlet of said fuel combustor to pass through said fuelcombustor for combustion.

In another aspect, an integrated adsorptive gas separation system forseparating at least a portion of a combustion gas mixture is providedaccording to an embodiment of the present invention, said combustion gasmixture comprising at least a first component comprising carbon dioxideand a second component, the system comprising:

-   -   a fuel combustor comprising a combustor air inlet, a combustion        chamber and a combustion gas outlet, wherein said combustion gas        comprises at least first and second components;    -   an adsorptive gas separator comprising an inlet and an outlet        end, wherein said adsorptive gas separator is fluidly connected        to said fuel combustor to receive said combustion gas as a feed        gas mixture into said inlet end and to adsorb at least a portion        of said first component onto at least one adsorbent material        comprised in said adsorbent gas separator; and    -   a combustion gas recycle fluid conduit which is fluidly        connected to said adsorptive gas separator and to said combustor        air inlet, and adapted to receive a desorbed combustion recycle        gas comprising at least a portion of said first component        adsorbed on said adsorbent material, and to return said desorbed        combustion recycle gas to said combustor air inlet.

It is a further object of the invention to provide an integrated fossilfuel combustion system including at least one of a PPSA and a PSA gasseparation process for separating carbon dioxide from a combustion gasmixture according to the present invention that addresses some of thelimitations of the prior art. In one embodiment of the presentinvention, an integrated adsorptive gas separation process forseparating at least a portion of a combustion gas mixture from a fuelcombustor is provided. In such embodiment, said combustion gas mixturecomprises at least carbon dioxide and nitrogen components and theprocess comprises the steps of:

admitting said combustion gas mixture into an adsorptive gas separationsystem;

admitting said combustion gas mixture into an inlet end of at least oneadsorbent contactor comprising at least one adsorbent material;

adsorbing at least a portion of said carbon dioxide combustion gascomponent on at least one said adsorbent material;

recovering a first product gas depleted in said carbon dioxide componentrelative to said combustion gas mixture from an outlet end of saidadsorbent contactor;

desorbing a first portion of said carbon dioxide component adsorbed onat least one said adsorbent material;

recovering a desorbed second product gas enriched in said carbon dioxidecomponent from at least one of said inlet and outlet ends of saidadsorbent contactor;

admitting a conditioning fluid into said adsorbent contactor anddesorbing a second portion of said carbon dioxide component adsorbed onat least one said adsorbent material to recover a carbon dioxideenriched conditioning stream; and

recycling at least a portion of said carbon dioxide enrichedconditioning stream recovered from said adsorbent contactor to an airinlet of said fuel combustor to pass through said fuel combustor forcombustion.

In a further embodiment of the present invention, the step of desorbinga first portion of said carbon dioxide component may comprise desorbinga first portion of said carbon dioxide component adsorbed on at leastone said adsorbent material by at least one of:

thermal swing desorption by heating at least one said adsorbentmaterial;

pressure swing desorption; and

partial pressure swing desorption.

In another embodiment of the present invention, an integrated adsorptivegas separation system for separating at least a portion of a combustiongas mixture is provided. In such an embodiment, the combustion gasmixture comprises at least carbon dioxide and nitrogen components, andthe adsorptive gas separation system comprises:

-   -   a fuel combustor comprising a combustor air inlet, a combustion        chamber and a combustion gas outlet, wherein said combustion gas        comprises at least carbon dioxide and nitrogen components;    -   an adsorptive gas separator comprising at least one adsorbent        contactor having an inlet and an outlet end, wherein said        adsorptive gas separator is fluidly connected to said fuel        combustor to receive said combustion gas as a feed gas mixture        into said inlet end of said at least one adsorbent contactor and        to adsorb at least a portion of said carbon dioxide component        onto at least one adsorbent material comprised in said adsorbent        contactor; and        a combustion gas recycle fluid conduit which is fluidly        connected to said adsorptive gas separator and to said combustor        air inlet, and adapted to receive a desorbed combustion recycle        gas comprising at least a portion of said carbon dioxide        component adsorbed on said adsorbent material, and to return        said desorbed combustion recycle gas to said combustor feed        inlet.

Further advantages of the invention will become apparent whenconsidering the drawings in conjunction with the detailed description.

5. BRIEF DESCRIPTION OF THE DRAWINGS

The systems and methods for integrated adsorptive gas separation ofcombustion gases according to embodiments of the present invention willnow be described with reference to the accompanying drawing figures, inwhich:

FIG. 1 illustrates a schematic view of an integrated adsorptive gasseparation system for separation of combustion gases from a gas turbinefor use in accordance with an embodiment of the present invention.

FIG. 2 illustrates a further schematic view of an integrated adsorptivegas separation system for separation of combustion gases from a gasturbine for use in accordance with an embodiment of the invention.

FIG. 3 illustrates yet a further schematic view of an integratedadsorptive gas separation system for separation of combustion gases froma gas turbine for use in accordance with an embodiment of the invention.

FIG. 4 illustrates a schematic view of an integrated adsorptive gasseparation system for separation of combustion gases from a fossil fuelcombustion process comprising a heat recovery steam generator (HRSG)comprising a steam loop for use in the gas separation system inaccordance with a further embodiment of the invention.

Like reference numerals refer to corresponding parts throughout theseveral views of the drawings.

6. DETAILED DESCRIPTION OF THE INVENTION

In one embodiment of the present invention, an integrated adsorptive gasseparation process is provided for separating at least a portion of acombustion gas mixture from a fuel combustor, wherein the combustion gasmixture comprises at least carbon dioxide and nitrogen components. Inone such embodiment, the adsorptive gas separation process may comprisea thermal swing adsorption (hereinafter “TSA”) process, wherein at leastone desorption step for desorption of a combustion gas componentadsorbed on an adsorbent material is driven primarily by thermal heatingof the adsorbent material, although secondary desorptive mechanisms suchas purge or displacement purge with a purge fluid may also be used indesorption of adsorbed components. In another such embodiment, theadsorptive gas separation process may comprise a pressure swingadsorption (hereinafter “PSA”) process, wherein at least one desorptionstep for desorption of a combustion gas component adsorbed on anadsorbent material is driven primarily by a swing in pressure of theadsorbent contactor comprising the adsorbent material, althoughsecondary adsorptive mechanisms such as purge or displacement purge witha purge fluid, or thermal heating of the adsorbent material may also beused in desorption of adsorbed combustion gas components, for example.In yet another such embodiment, the adsorptive gas separation processmay comprise a partial pressure swing adsorption (hereinafter “PPSA”)process, wherein at least one desorption step for desorption of acombustion gas component adsorbed on an adsorbent material is drivenprimarily by a swing or difference in partial pressure or concentrationof at least one adsorptive gas component in the adsorbent contactorcomprising the adsorbent material, although secondary adsorptivemechanisms such as thermal heating of the adsorbent material or pressureswing may also be used in desorption of adsorbed combustion gascomponents, for example.

In one embodiment according to the present invention, the fuel combustormay comprise any suitable type of fuel combustion device which usesprimarily ambient air as a source of combustion air, such as but notlimited to gaseous fuel, liquid fuel and/or solid fuel combustors. In aparticular embodiment, the fuel combustor may comprise at least one of:a gas turbine combustor, combined cycle gas turbine combustor,liquid-fuel (such as oil/kerosene/diesel and other liquid fuel fired)combustor, coal-fired combustor (including solid, pulverized, gasifiedor other forms of coal-fueled combustors such as coal-fired powergeneration plants), biomass solid and/or liquid fuel combustor, steamgenerator/boiler combustor, and process heater combustor (such as may beused in refinery and/or industrial processes to heat process fluidsand/or gases), for example.

In one embodiment, the integrated adsorptive gas separation process maycomprise an initial step of admitting the combustion gas mixture from afuel combustor and comprising at least carbon dioxide and nitrogencomponents, as a feed mixture, into an adsorptive gas separation system.The combustion gas mixture may then be admitted into the inlet end of atleast one adsorbent contactor comprising at least one adsorbentmaterial. The process may then comprise adsorbing at least a portion ofthe carbon dioxide combustion gas component on the adsorbent material.Following adsorption, a first product gas depleted in said carbondioxide gas component relative to the feed mixture may be recovered froman outlet end of the adsorbent contactor. In a preferred embodiment, theadsorption step may desirably result in substantially all of the carbondioxide combustion gas component of the combustion gas being adsorbed onthe adsorbent material in the adsorptive gas separation system, so thatthe first product gas recovered from the adsorbent contactor maydesirably be substantially free of carbon dioxide. In one suchembodiment, the at least substantially complete removal of carbondioxide from the combustion gas mixture may be desirable to allow thefirst product gas to be released as a flue gas into the environmentsubstantially free of carbon dioxide, such as to reduce carbon emissionsfrom the operation of the fuel combustor. In a particular suchembodiment, the first product gas may desirably have a carbon dioxideconcentration that is less than the ambient carbon dioxide concentrationof the environment, such as below the approximately 390 ppm carbondioxide concentration of the atmosphere, so that the released firstproduct flue gas from the adsorption process may in net effect removecarbon dioxide from the atmosphere.

In one embodiment, the integrated adsorptive gas separation process maythen comprise desorbing a first portion of the carbon dioxide componentadsorbed on the at least one adsorbent material by heating the at leastone adsorbent material. As noted above, in one embodiment, thedesorption of adsorbed carbon dioxide may be primarily thermally drivenas a TSA process, but may also be assisted by one or more secondarydesorption mechanisms such as a pressure swing desorption, partialpressure desorption and/or purge desorption mechanism, for example. Thenthe process may comprise recovering a desorbed second product gasenriched in carbon dioxide from either the inlet or outlet end of theadsorbent contactor. Alternatively, the desorption of adsorbed carbondioxide may be primarily driven by one or more of a pressure swingand/or partial pressure swing process, in combination or in place of aTSA process, for example.

In a preferred embodiment, only a portion of the adsorbed carbon dioxideis desorbed from the contactor and recovered in the second product gas,so that at least a portion of the carbon dioxide remains adsorbed on theadsorbent contactor. In a particular preferred embodiment, the desorbedportion of carbon dioxide recovered in the second product gas maycomprise only about a third of the total adsorbed carbon dioxide,leaving about two thirds of the carbon dioxide component adsorbed on theadsorbent contactor at the end of the first desorption step. Therefore,because only a portion of the adsorbed carbon dioxide is desorbed in thefirst desorption step, the amount of heat energy required to desorb itis much reduced compared to processes where the majority orsubstantially all of the adsorbed carbon dioxide is desorbed. In apreferred embodiment, steam may be used to heat the adsorbent materialand desorb the first portion of carbon dioxide such as by heating and/ordisplacement purge desorptive mechanisms, and accordingly, asignificantly reduced amount of steam may desirably be required todesorb only about a third of the adsorbed carbon dioxide from theadsorbent contactor. In one such preferred embodiment, the desorbedsecond product gas desirably comprises substantially pure carbondioxide, or in the case of steam being used to purge the adsorbentcontactor during desorption, comprises substantially only carbon dioxideand steam. Accordingly, such second product gas is desirably highlyconcentrated in carbon dioxide and thereby suitable to be compressedefficiently (with condensation knockout of any steam component) for useand/or storage such as for carbon sequestration or other applicationssuch as enhanced oil recovery purposes to reduce carbon emissions fromthe operation of the fuel combustor.

Following the first desorption, the integrated adsorptive gas separationprocess may comprise admitting ambient air or alternatively anothersuitable conditioning gas stream into the adsorbent contactor anddesorbing a second portion of the carbon dioxide component adsorbed onthe at least one adsorbent material in the contactor to recover a carbondioxide enriched air or conditioning stream. In one embodiment, thedesorption of the second portion of the carbon dioxide component may bedriven by at least one of a TSA, PSA and PPSA desorption process. Atleast a portion of the carbon dioxide enriched air and/or conditioningstream is then recycled to the air inlet of the fuel combustor to passthrough the combustor for combustion. In one such embodiment, the carbondioxide enriched air stream may desirably have a higher carbon dioxideconcentration than the ambient air, such as a carbon dioxideconcentration above the about 400 ppm atmospheric carbon dioxideconcentration, for example. In a preferred embodiment, the admittedambient air may desirably be effective to desorb a majority, or morepreferably, substantially all of the remaining carbon dioxide adsorbedon the adsorbent material, and to recycle the second portion of carbondioxide into the combustion air intake of the fuel combustor.

A primary benefit of the recycling of the second portion of the adsorbedcarbon dioxide to the intake of the fuel combustor is to increase theconcentration of carbon dioxide in the post-combustion gas mixture whichis admitted to the adsorptive gas separation system as the feed mixture,since the combustion gas will contain both the recycled carbon dioxide,as well as the carbon dioxide generated in the combustion process.Particularly in the case of fuel combustors where the baseline carbondioxide content of the combustion gas mixture is relatively low, such asfor gas turbines, and in an additional embodiment in some coal-firedthermal combustors, steam generators/boiler, process heaters, forexample, such an increase in combustion gas carbon dioxide content maydesirably increase the efficiency of the adsorptive separation of carbondioxide in the adsorptive gas separation system compared to anon-recycled combustion gas mixture more dilute in carbon dioxide. Suchincreased efficiency of adsorptive carbon dioxide separation resultingfrom the increased carbon dioxide concentration in the combustion gasprovided as a feed mixture in embodiments of the present invention maydesirably allow for at least one of: decreased energy consumption fordesorption of adsorbed carbon dioxide such as in the form of decreasedsteam or other purge fluid consumption or desorption heating; increasedcarbon dioxide purity in the desorbed second product gas enriched incarbon dioxide; reduced size and/or capital cost of the adsorptiveseparation system, and improved system recovery of carbon dioxide, forexample.

In a particular embodiment, the desorption of the second portion ofcarbon dioxide is accomplished primarily by displacement purge by theambient air and/or other conditioning stream, and in such a case theenergy required for desorbing the carbon dioxide may be desirably small.Also, in one such preferred embodiment, the air and/or conditioningstream used to desorb the second portion of carbon dioxide may alsodesirably be cooled by the effect of the heat of desorption of thecarbon dioxide, and therefore may be advantageously cooler and denserwhen recycled to the combustor air intake than available surroundingambient air, which may desirably improve the efficiency of the fuelcombustor, such as in the case where the fuel combustor operates atsupra-atmospheric pressures, such as gas turbine combustors, where thecombustion air is compressed before combustion, for example. In afurther embodiment, the increased carbon dioxide in the combustor inletmixture due to recycle of carbon dioxide from the adsorption system maydesirably provide for an increased heat capacity of the inlet mixturerelative to ambient inlet air. Such increased heat capacity of thecombustor inlet mixture may desirably allow for a decrease in thenon-combusted excess air portion of the inlet mixture which is requiredto maintain combustion temperatures below critical levels in fuelcombustors such as gas turbines, for example, which may desirablyincrease efficiency of the gas turbine due to reduced inlet mass flow orenable increased fuel firing rate thereby increasing net power output,for example.

In an alternative embodiment where the fuel combustor operates atsubstantially atmospheric pressures, such as in coal-fired, steamgenerator/boiler, or process heater combustors, the air used to desorbthe second portion of carbon dioxide may instead be heated by thecomparatively hot adsorbent contactor and/or adsorbent material duringthe desorption step. In such case, the carbon dioxide enrichedconditioning air stream recycled to the combustor air inlet mayadvantageously be heated above ambient air temperature, and maydesirably improve the efficiency of the atmospheric fuel combustor.

In a further embodiment, in fuel combustors which include heat transferor recovery from combustion flue gas, such as combined cycle gasturbines, thermal power plants, steam generators/boilers, processheaters, and the like, the increase in carbon dioxide concentration inthe post-combustion flue gas due to recycling of a portion of theadsorbed carbon dioxide to the combustor inlet may also desirablyincrease the heat capacity of the post-combustion flue gas, due to thehigher heat capacity of carbon dioxide compared to air. Such an increasein the heat capacity of the post-combustion flue gas may desirably allowfor greater convective heat transfer efficiency in the heattransfer/recovery portion of the combustion system, such as in heatexchangers and/or heat recovery steam generator (HRSG) systems, forexample.

In yet a further embodiment, in fuel combustors which include radiantheat transfer or recovery from combustion flue gas, such as steamgenerators/boilers, process heaters, and some thermal power plants andthe like, the increase in carbon dioxide concentration in thepost-combustion flue gas due to recycling of a portion of the adsorbedcarbon dioxide to the combustor inlet may also desirably increase theradiant heat transfer capacity of the post-combustion flue gas, due tothe IR emission spectrum of the increased concentration carbon dioxidecomponent of the flue gas, relative to the negligible radiant heattransfer capacity of the air component of the flue gas. Such an increasein the radiant heat transfer capacity of the post-combustion flue gasmay desirably allow for greater radiant heat recovery in the radiantzone of heat exchangers in such combustors, for example.

In another embodiment, the increase in carbon dioxide concentration inthe post-combustion flue gas due to recycling of a portion of theadsorbed carbon dioxide to the combustor inlet may also desirably resultin a lower adiabatic flame temperature of combustion relative to a lowercarbon dioxide concentration inlet mixture, which may desirably resultin reduced nitrogen oxide production in the combustion process. Suchreduced nitrogen oxides in the combustion flue gas may be desirable toimprove emissions quality and/or to reduce requirements for emissiontreatment systems, for example.

In another embodiment of the present invention, water vapor in the formof steam used in desorption of carbon dioxide from the adsorbentmaterial may be provided for recycle to the combustor inlet mixture,such as for application to fuel combustors implementing water injectionin the pre-combustion inlet mixture. In such an embodiment, requirementsfor water injection may be desirably decreased by such use of desorptionwater vapor recycled from the adsorption process, and/or recovery ofwater from steam purge desorption steps may be increased, for example.The present integrated adsorptive gas separation process according tothe above embodiments may then desirably be repeated to provide for acontinuous or repeated cyclic combustion gas separation method forseparating a first portion of the carbon dioxide component from thecombustion gas mixture, such as for carbon sequestration purposes. Inparticular, an adsorptive gas separation system for operation accordingto the present integrated gas separation method may desirably comprisetwo or more adsorbent contactors, so as to provide for staggeredoperation of the present integrated gas separation method and allowcontinuous and/or semi-continuous adsorptive separation from thecombustion gas of the fuel combustor. In particular, an integratedadsorptive separation system may comprise three or more adsorbentcontactors such that the first product fluid may be recovered from onecontactor while the desorbed second product fluid is recovered from thesecond contactor, and the carbon dioxide enriched conditioning airstream is recovered from the third contactor. Any suitable mechanicalarrangement may be implemented in the integrated adsorptive separationsystem to provide for and control the fluid flows required forimplementation of the integrated gas separation process of the presentembodiment, such as an adsorptive separation system usingmechanical/pneumatic or other types of valves or other flow controldevices for example to implement the fluid flows of the steps of thepresent TSA and/or PPSA and/or PSA adsorption process, as are known inthe art for systems comprising one, two, or three or more adsorberscontaining adsorbent material. In a particular embodiment, a rotarywheel or rotor mechanical arrangement where the adsorbers containingadsorbent material are located in the rotating component may beimplemented to provide for and control the fluid flows required toimplement the integrated gas separation process of the invention, suchas may be similar to those used in a rotary enthalpy or other adsorbentwheel, for example.

In a particular embodiment, the one or more adsorbent contactors maycomprise parallel passage adsorbent contactors. In such an embodiment,suitable such parallel passage adsorbent contactors may comprise aplurality of substantially parallel fluid flow passages oriented in afirst axial direction between an inlet and outlet end of the contactorin order to permit fluid to flow through the contactor, and cell wallswhich comprise at least one adsorbent material situated between andseparating the fluid flow passages. The parallel passage adsorbentcontactor may also desirably comprise a plurality of axially continuousthermally conductive filaments oriented in the axial direction of thecontactor and in direct contact with the at least one adsorbent materialcomprised in or on the cell walls of the contactor. Certain suchparallel passage adsorbent contactor structures which may be suitablefor use in implementing the integrated combustion gas separation processaccording to an embodiment of the present invention are described in theapplicant's co-pending PCT international patent application filed asPCT/CA2010/000251 on Feb. 26, 2010, the contents of which are hereinincorporated by reference as though they had formed part of thisapplication as presently filed.

FIG. 1 illustrates a schematic view of an exemplary integratedadsorptive gas separation system 10 for separation of combustion gasesfrom a gas turbine 30 for use in accordance with an embodiment of thepresent invention. In one embodiment, the integrated adsorptive gasseparation system 10 may be used for implementing the present integratedcombustion gas separation process described above. The system 10comprises a gas turbine 30, such as a natural gas power generationturbine, for example. Turbine 30 comprises an air inlet 36 for admittingair into the turbine 30 for admixture with fuel 32 in a combustionchamber to produce a combustion gas or flue gas mixture comprising atleast carbon dioxide and nitrogen components which is exhausted from theturbine 30.

In a preferred embodiment of the integrated adsorptive gas separationsystem 10, gas turbine 30 is a combined cycle gas turbine (CCGT) andalso comprises a heat recovery steam generator (HRSG) 40 which receivescombustion gas from the turbine 30 and raises steam which is expandedover one or more heat recovery expansion turbines to recover heat energyand generator power. Following such use in the HRSG 40 to generatesteam, combustion gas exits the HRSG 40 from combustion gas outlet 41.In one such embodiment, the HRSG 40 may also comprise a low pressuresteam outlet 48 for supplying low pressure steam to an inlet 25 ofadsorptive gas separation system 20. In another preferred embodiment,the integrated adsorptive gas separation system 10 also comprises acooler 50 such as a direct contact cooler 50 which receives combustiongas from the outlet 41 of the HRSG 40 and cools the combustion gas foruse as a feed mixture to inlet 24 of the adsorptive gas separationsystem 20.

Adsorptive gas separation system 20 comprises one or more adsorptivecontactors, each comprising at least one suitable adsorbent material. Ina preferred embodiment, separation system 20 may comprise at least threeadsorptive contactors 21, 22 and 23. In one embodiment, a firstcontactor 21 may receive cooled combustion gas mixture at inlet 24, foradsorption of the carbon dioxide component of the combustion gas on theadsorbent material of contactor 21, to recover a first product gas,desirably depleted of carbon dioxide from outlet 29. In one suchembodiment, the first product gas may comprise flue gas substantiallyfree of carbon dioxide, such as for release to the environment. A secondcontactor 22 may desorb a first portion of adsorbed carbon dioxide byheating of the adsorbent material, such as by admission of low pressuresteam through inlet 25, to recover a second product gas stream desirablyenriched in carbon dioxide through outlet 28. In one embodiment, thesecond product gas stream may comprise substantially pure carbon dioxideand/or carbon dioxide and steam (or other suitable purge fluid), whichmay be efficiently compressed such as for use and/or storage such as forcarbon sequestration or alternate use in enhanced oil recovery, forexample. A third contactor 23 may receive an air purge stream throughinlet 26 such as to desorb a second portion of carbon dioxide from theadsorbent material in the contactor 23, to recover a recycleconditioning air stream enriched in carbon dioxide through outlet 27,for recycle to the inlet 36 of gas turbine 30 to be used as a portion ofthe combustion air passing into turbine 30 for combustion.

In such an embodiment, the first adsorber 21 preferably adsorbssubstantially all of the carbon dioxide component of the combustion gasentering inlet 24, resulting in a first product gas recovered fromoutlet 29 that is substantially free of carbon dioxide. Further, in apreferred embodiment, the first portion of carbon dioxide desorbed fromsecond contactor 22 may desirably comprise no more than half of thetotal carbon dioxide adsorbed from the combustion gas, and moredesirably may comprise about one third of the total adsorbed carbondioxide. Accordingly, then, the second portion of carbon dioxidedesorbed from third contactor 23 may desirably comprise no less thanhalf of the total carbon dioxide adsorbed from the combustion gas, andmore preferably about two thirds of the total adsorbed carbon dioxide.In such preferred embodiments, the desorption and recycle of preferablyno less than half, and more preferably about two thirds of the totaladsorbed carbon dioxide back to the inlet 36 of gas turbine 30 mayadvantageously increase the concentration of carbon dioxide in thecombustion gas delivered to the gas separation system 20, therebyincreasing the efficiency of carbon dioxide adsorption in firstcontactor 21 and also increase the efficiency of desorption of the firstportion of carbon dioxide in second contactor 22, thereby increasing theenergy efficiency of the gas separation system 20 and decreasing thecost of producing first and second product gases depleted and enrichedin carbon dioxide, respectively. Further, the recycle of carbon dioxideand air back to the turbine intake 36 may also have the benefit ofreducing the temperature of the recycled intake gas, due to the decreasein temperature of the intake gas from the heat of desorption of thesecond portion of carbon dioxide, thereby increasing the efficiency ofthe gas turbine 30. Also, in one embodiment, the efficiency of thecompression stage of the turbine 30 may also be desirably increased dueto the increased heat capacity of carbon dioxide relative to air in therecycled portion of the air flowing into turbine intake 36.

FIGS. 2 and 3 illustrates further schematic views of an exemplaryintegrated adsorptive gas separation system 100 for separation ofcombustion gases from a gas turbine 300 for use in accordance withembodiments of the present invention. In one embodiment, the integratedadsorptive gas separation system 100 may be used for implementing thepresent integrated combustion gas separation process described above,similar to the gas separation system illustrated in FIG. 1. The system100 comprises a gas turbine 300, such as a natural gas power generationturbine, suitable examples of which may include natural gas powergeneration turbines manufactured by General Electric Company, ofSchenectady, N.Y., USA, for example. Turbine 300 comprises an air inlet306 for admitting air into the turbine 300 for admixture with fuel 302(typically natural gas comprising primarily methane, but may include anyother suitable gaseous, vapor, liquid, or airborne combustible fuel) ina combustion chamber to produce a combustion gas or flue gas mixturecomprising at least carbon dioxide and nitrogen components which isexhausted from the turbine 300, through turbine combustion gas exhaustoutlet 304.

In a preferred embodiment of the integrated adsorptive gas separationsystem 100, gas turbine 300 is a combined cycle gas turbine (CCGT) andalso comprises a heat recovery steam generator (HRSG) 400 which receivescombustion gas from exhaust outlet 304 of the turbine 300 and uses theheat of the combustion gas exhaust to raise steam which is expanded overmultiple heat recovery expansion steam turbines to recover heat energyand generator power. In the present embodiment, HRSG may desirablycomprise high temperature steam turbine 402, intermediate pressure steamturbine 404 and low pressure steam turbine 406 operating sequentially soas to extract energy from the steam raised by cooling the combustion gasexhaust from turbine 300. Following such use in the HRSG 400 to generatesteam, combustion gas exits the HRSG 400 from combustion gas outlet 410.In one such embodiment, the HRSG 400 may also comprise a low pressuresteam outlet 408 for supplying low pressure steam from the outlet of lowpressure steam turbine 406 to an inlet 214 of adsorptive gas separationsystem 200. In another preferred embodiment, the integrated adsorptivegas separation system 100 also comprises a combustion gas cooler 220such as a direct contact combustion gas cooler 220 which receivescombustion gas from the outlet 410 of the HRSG 400 and cools thecombustion gas for use as a feed mixture to inlet 212 of the adsorptivegas separation system 200.

Adsorptive gas separation system 200 comprises one or more adsorptivecontactors, each comprising at least one suitable adsorbent material. Ina preferred embodiment, separation system 200 may comprise at leastthree adsorptive contactors 202, 204 and 206. In one embodiment, anexemplary first contactor 202, which in a preferred embodiment maycomprise a parallel passage adsorbent contactor 202 may receive cooledcombustion gas mixture at inlet 212, for adsorption of the carbondioxide component of the combustion gas on the adsorbent material ofcontactor 202, to recover a first product gas, desirably depleted ofcarbon dioxide, from outlet 222. In one such embodiment, the firstproduct gas may desirably comprise combustion flue gas substantiallyfree of carbon dioxide, such as for release to the environment. A secondcontactor 204 may desorb a first portion of adsorbed carbon dioxide fromthe adsorbent material, such as by heating of the adsorbent material. Inone such embodiment, the first portion of carbon dioxide may be desorbedby heating the adsorbent material through the admission of low pressuresteam through inlet 214, to recover a second product gas streamdesirably enriched in carbon dioxide through outlet 224. In another suchembodiment, an alternative or additional source of heat for heating theadsorbent material to desorb the first portion of carbon dioxide may beprovided by heated combustion flue gas, such as sourced from downstreamfrom the gas turbine 300, for example. In one embodiment, the secondproduct gas stream may comprise substantially pure carbon dioxide and/orcarbon dioxide and steam (or other suitable purge fluid), which may bedesirably be suitable to be efficiently compressed such as for useand/or storage such as for carbon sequestration or alternate use inenhanced oil recovery, for example. A third contactor 206 may receive anair purge stream through inlet 216 such as to desorb a second portion ofcarbon dioxide from the adsorbent material in the contactor 206, torecover a recycle conditioning air stream enriched in carbon dioxidethrough outlet 226, for recycle to the inlet 306 of gas turbine 300 tobe used as at least a portion of the combustion air passing into turbine300 for combustion.

In such an embodiment, the first adsorbent contactor 202 preferablyadsorbs substantially all of the carbon dioxide component of thecombustion gas entering inlet 212, resulting in a first product gasrecovered from outlet 222 that is substantially free of carbon dioxide.Further, in a preferred embodiment, the first portion of carbon dioxidedesorbed from second contactor 204 may desirably comprise no more thanhalf of the total carbon dioxide adsorbed from the combustion gas, andmore desirably may comprise about one third of the total adsorbed carbondioxide. Accordingly, then, the second portion of carbon dioxidedesorbed from third contactor 206 may desirably comprise no less thanhalf of the total carbon dioxide adsorbed from the combustion gas, andmore preferably about two thirds of the total adsorbed carbon dioxide.In such preferred embodiments, the desorption and recycle of preferablyno less than half, and more preferably about two thirds of the totaladsorbed carbon dioxide back to the inlet 306 of gas turbine 300 mayadvantageously increase the concentration of carbon dioxide in thecombustion gas delivered to the gas separation system 200, therebyincreasing the efficiency of carbon dioxide adsorption in firstcontactor 202 and also increase the efficiency of desorption of thefirst portion of carbon dioxide in second contactor 204, therebyincreasing the energy efficiency of the gas separation system 200 anddecreasing the cost of producing first and second product gases depletedand enriched in carbon dioxide, respectively. Further, the recycle ofcarbon dioxide and air back to the turbine intake 306 may also have thebenefit of reducing the temperature of the recycled intake gas, due tothe decrease in temperature of the intake gas from the heat ofdesorption of the second portion of carbon dioxide, thereby increasingthe efficiency of the gas turbine 300. Also, in one embodiment, theefficiency of the compression stage of the turbine 300 may also bedesirably increased due to the increased heat capacity of carbon dioxiderelative to air in the recycled portion of the air flowing into turbineintake 306 from the adsorptive gas separation system 200.

In one embodiment of the above-noted invention, the second produce gasrecovered from outlet 224 of the gas separation system 200 and enrichedin carbon dioxide may desirably be fluidly connected to a carbon dioxidecompression train system 240. The carbon dioxide compression train 240may desirably be suitable to compress the carbon dioxide rich secondproduct gas, such as through a series of sequential compression stages,to provide a highly pressurized and/or liquefied concentrated carbondioxide product gas 230 such as for export to other industrial and/orsequestration uses, such as sequestered storage and/or enhanced oilrecovery, for example.

In a particular embodiment of the present invention adapted toadsorptive gas separation of combustion gas from a combined cyclenatural gas power generation turbine, the adsorptive gas separationsystem may desirably separate about one third of the carbon dioxide fromthe gas turbine combustion gas into the carbon dioxide rich firstproduct gas, such that about two thirds of the carbon dioxide from theturbine combustion gas is recycled back to the gas turbine intake in therecycle conditioning air stream. In one such embodiment comprisingapproximately two thirds recycle of carbon dioxide, the carbon dioxideconcentration of the turbine combustion gas may be desirably controlledto be about 12% carbon dioxide, wherein approximately 4% of the 12%carbon dioxide content is removed in the carbon dioxide rich secondproduct gas (such as for sequestration and/or industrial use, forexample) and approximately 8% of the 12% carbon dioxide content isrecycled back to the intake of the turbine. In alternative embodiments,the carbon dioxide concentration of the turbine combustion gas may bedesirably controlled to be substantially higher than 12% carbon dioxide,such as up to about 50% carbon dioxide for example in turbines which aresuitably configured for such carbon dioxide concentrations, such as maybe additionally advantageous to further increase efficiency ofadsorptive separation of carbon dioxide in the adsorption system, and/orincrease efficiency of turbine combustion and/or heat recoveryprocesses, for example.

FIG. 4 illustrates a schematic view of a portion of an integratedadsorptive gas separation system 400 for separation of combustion gasesfrom a fossil fuel combustion process comprising a heat recovery steamgenerator (HRSG) 402 according to an embodiment of the presentinvention. The HRSG 402 of the system of FIG. 4 comprises threeexemplary heat recovery steam generation and expansion low loopsincluding a high pressure steam loop 404 receiving boiler feed water(BFW) 403 at a first high pressure, and passing steam generated throughhigh pressure expander 406 to capture additional energy from thecombustor flue gas. HRSG 402 also similarly comprises medium steam loop408 receiving BFW from source 405 at a medium pressure, and recoveringenergy from passing the steam through medium pressure expander 410. Alsosimilarly, HRSG 402 further comprises a low pressure steam loop 414receiving BFW from source 407 and passing generated steam through lowpressure expander 412.

HRSG 402 additionally comprises an auxiliary very low pressure loop 416which receives BFW from source 409 at a very low pressure. In theparticular embodiment shown in FIG. 4, the steam generated in very lowpressure loop 416 may desirably be supplied to the adsorption separationsystem (not show) such as through very low pressure steam outlet 420,without passing through an expansion step following loop 416. In such anembodiment, the lowest pressure steam loop 416 may desirably beconfigured to provide a supply of steam at a relatively lower pressurethan the rest of the HRSG 402, such as may be suitable only for lowpressure use in the adsorptive gas separation system (not shown) whichpreferably operates at substantially ambient pressure or only slightlyabove, for example. The lowest pressure steam provided from theexemplary lowest pressure steam loop 416 may desirably be used toprovide a steam purge fluid such as for use in desorption of carbondioxide from the adsorbers of the adsorptive separation system, such asfor desorption of a carbon dioxide enriched product gas and/or forrecycle to the inlet of the fuel combustor for combustion, as describedabove in reference to other embodiments of the invention.

In such an embodiment, the generation and use of very low pressure steamfrom lowest pressure steam loop 416 for desorbing adsorbed gas such ascarbon dioxide from the adsorbers of the gas separation system maydesirably consume less energy in the generation of such steam in theauxiliary lowest pressure loop 416, compared with an embodiment wheresuch purge fluid steam was generated in another higher pressure loop ofthe HRSG 402, such as at an elevated pressure level within the commonexisting high, medium or low pressure steam generation loopsin aconventional HRSG, for example. In a conventional such HRSG, a sourcefor steam to be used for desorption in the gas separation system may forexample receive steam from a conventional low pressure steam loop 414,which may undesirably reduce the steam available to use in for expansionin a low pressure expander 412, for example.

In an alternative aspect according to the present invention, theintegrated adsorptive gas separation process according to an embodimentof the invention may comprise a temperature swing adsorption (TSA)process particularly directed to separating carbon dioxide gas from acombustion gas feed mixture from a fuel combustor, where in thecombustion gas mixture comprises at least carbon dioxide and nitrogencomponents. In one such embodiment, the TSA process for separatingcarbon dioxide may be adapted for removing at least a portion of carbondioxide from the combustion gas or exhaust of a thermal power plant,such as a coal or natural gas power plant for example, or from a steamgenerator/boiler or process heater. In such embodiments, the removal ofonly a portion of the carbon dioxide content of the combustion gas to berecovered in the second product gas may desirably have the advantage ofincreasing the concentration of carbon dioxide in the combustion gasexiting from the fuel combustor, such that carbon dioxide from thecombustion gas in the adsorptive gas separation system may be moreefficiently adsorptively separated such as by a TSA process. In anotheroptional embodiment, the adsorptive carbon dioxide gas separationprocess may be based primarily on a pressure swing and/or a partialpressure swing/displacement purge adsorption process, such as describedabove in reference to other embodiments where TSA is not the primaryadsorptive process but may comprise a secondary adsorptive driver, forexample.

In one embodiment of the present invention, a TSA (or alternatively aPSA and/or PPSA) carbon dioxide separation process may desirably berepeated in each of multiple parallel passage adsorbent contactors inthe adsorptive gas separation system to provide for a continuous orrepeated cyclic separation method for separating a portion of the carbondioxide from the combustion gas feed mixture, while recycling a portionof the carbon dioxide to the air inlet of the fuel combustor. Inparticular, similar to as described above in other embodiments, anadsorptive gas separation system for operation according to anembodiment of the present invention may desirably comprise two or moresuch parallel passage adsorbent contactors, so as to provide forstaggered operation of a suitable TSA (or alternatively a PSA and/orPPSA) separation process and allow continuous and/or semi-continuousadsorptive separation from a source of fuel combustor source ofcombustion gas. As described above, any suitable known adsorptiveseparation system using mechanical/pneumatic or other types of valves orother flow control devices for example may be used to implement the gasflows of the steps of the present TSA (or alternatively a PSA and/orPPSA) process, as are known in the art for systems comprising one, two,or three or more adsorbers containing adsorbent material.

Similar to as described above, in one embodiment of the presentinvention, an adsorptive gas separation system suitable for implementingthe carbon dioxide separation process comprises at least one parallelpassage adsorbent contactor which each comprise a plurality ofsubstantially parallel fluid flow passages oriented in a first axialdirection between and inlet and outlet end of the contactor in order topermit gas to flow through the contactor, and cell walls which compriseat least one carbon dioxide selective adsorbent material situatedbetween and separating the fluid flow passages. Each suitable suchparallel passage adsorbent contactor further comprises a plurality ofaxially continuous thermally conductive filaments oriented in the axialdirection of the contactor and in direct contact with the at least onecarbon dioxide adsorbent material comprised in the cell walls of thecontactor. As described above, certain such parallel passage adsorbentcontactor structures which may be suitable for use in implementing a TSAcarbon dioxide separation process according to an embodiment of thepresent invention are described in the applicant's co-pending PCTinternational patent application filed as PCT/CA2010/000251, thecontents of which are herein incorporated by reference as though theyhad formed part of this application as originally filed. In anotheroptional embodiment, the adsorptive gas separation system may besuitable for implementing a carbon dioxide separation process basedprimarily on a pressure swing and/or a partial pressureswing/displacement purge adsorption process, such as described above inreference to other embodiments where TSA is not the primary adsorptiveprocess but may comprise a secondary adsorptive driver, for example.

In certain embodiments of the present integrated adsorptive combustiongas separation process, any suitable known carbon dioxide adsorbentmaterial may be used in the adsorbent contactor(s) of the adsorptiveseparation system to adsorb carbon dioxide during the adsorption step ofthe process. Potentially suitable such carbon dioxide adsorbents maycomprise, but are not limited to: activated carbon adsorbent, amineimpregnated adsorbent supports (comprising silica, activated carbon,alumina, zeolite, polymer and ceramic supports), metal salt, metalhydroxide, metal oxide, zeolite, hydrotalcite, silicalite, metal organicframework and zeolitic imadazolate framework adsorbent materials, andcombinations thereof. In a particular embodiment, a suitable carbondioxide adsorbent material may be selected that may also desirably beselective for the adsorption of carbon dioxide over any other gascomponents of the combustion gas feed mixture, for example.

Similar to as described above in other embodiments, in one embodiment ofthe present invention, the steps of a TSA (or alternatively or incombination with a PPSA) carbon dioxide gas separation process may bedesirably conducted under substantially constant or isobaric pressureconditions. In a particular embodiment, the admission of the combustiongas feed mixture to the adsorbent contactor, adsorption of carbondioxide, recovery of a flue gas product stream, desorption of a portionof carbon dioxide as a carbon dioxide second product stream, andrecovery of a second desorbed portion of carbon dioxide in a recycle airconditioning stream may all be conducted under substantially atmosphericpressure, for example. In an alternative embodiment, such steps of thepresent TSA (or alternatively or in combination with a PPSA) process maybe conducted at a substantially constant elevated pressure, such asunder isobaric super-atmospheric conditions, for example. In anotheralternative embodiment, the admitting, adsorbing and recovering a fluegas product stream steps of the present TSA (or alternatively or incombination with a PPSA) process may be conducted under a firstsubstantially constant pressure condition, such as under atmosphericpressure, for example, while the desorbing and recovering a desorbedcarbon dioxide second product steps may be conducted at an elevatedpressure, such as an elevated super-atmospheric pressure. In one suchembodiment, the adsorbent contactor may be substantially sealed prior tothe desorbing step, and the heating of the adsorbent contactor conductedduring the desorbing step may result in increased pressure within thecontactor as the adsorbed carbon dioxide desorbs from the adsorbentmaterial, thereby raising the pressure of the contactor to asuper-atmospheric level, for example. In this way the desorbed carbondioxide product fluid may optionally be recovered at a desirablyelevated pressure above the pressure at which the adsorbing steps wereconducted, so as to provide a pressurized carbon dioxide second productstream which may be desirable in certain applications, such as wherefurther compression of the carbon dioxide may be required for transport,storage, sequestration or industrial use.

In another optional embodiment, the adsorptive gas separation system mayreceive combustion gas from the fuel combustor (such as from the exhaustof the HRSG for a combined cycle gas turbine, or from the turbineexhaust for a gas turbine without HRSG) at a pressure elevated aboveambient pressure such as to provide sufficient pressure to supply anddrive the combustion gas through the separation system, for example. Inone such embodiment, the combustion gas may be provided to the gasseparation system at a suitable super-atmospheric pressure such asapproximately 10 kPa above ambient pressure, for example. In aparticular such embodiment, the provision of combustion gas at asufficiently elevated pressure to provide for driving the combustion gasthrough the separation system may desirably allow for removal ofauxiliary equipment such as a draft fan or other compressive equipmentassociated with the gas separation system for moving combustion gasthrough the separation system, for example, which may desirably reduceenergy consumption of the integrated gas separation system and fuelcombustor.

Further optional embodiments of the present inventive integratedadsorptive gas separation process and system particularly adapted forintegration with a natural gas combined cycle gas turbine powergenerator are contemplated which comprise at least partial recycle ofadsorbed carbon dioxide from the combustion gas stream back into theintake air of the gas turbine, as may be envisioned with other gasseparation techniques which may be known in the art.

The exemplary embodiments herein described are not intended to beexhaustive or to limit the scope of the invention to the precise formsdisclosed. They are chosen and described to explain the principles ofthe invention and its application and practical use to allow othersskilled in the art to comprehend its teachings.

As will be apparent to those skilled in the art in light of theforegoing disclosure, many alterations and modifications are possible inthe practice of this invention without departing from the scope thereof.Accordingly, the scope of the invention is to be construed in accordancewith the substance defined by the following claims.

What is claimed is:
 1. An integrated adsorptive gas separation process for separating at least a portion of a combustion gas mixture from a fuel combustor, said combustion gas mixture comprising at least a first component comprising carbon dioxide and a second component, the process comprising: admitting said combustion gas mixture into an adsorptive gas separation system comprising at least one adsorbent material; adsorbing at least a portion of said first component on at least one said adsorbent material; recovering a first product gas depleted in said first component relative to said combustion gas mixture from an outlet end of said adsorptive gas separation system; desorbing a first portion of said first component adsorbed on at least one said adsorbent material; recovering a desorbed second product gas enriched in said first component from at least one of said inlet and outlet ends of said adsorptive gas separation system; admitting a conditioning fluid into said adsorptive gas separation system and desorbing a second portion of said first component adsorbed on at least one said adsorbent material to recover a first component enriched conditioning stream; and recycling at least a portion of said first component enriched conditioning stream recovered from said adsorptive gas separation system to an air inlet of said fuel combustor to pass through said fuel combustor for combustion.
 2. The integrated adsorptive gas separation process according to claim 1, wherein said desorbing a first portion of said first component comprises desorbing a first portion of said first component adsorbed on at least one said adsorbent material by at least one of: thermal swing desorption by heating at least one said adsorbent material; pressure swing desorption; and partial pressure swing desorption.
 3. The integrated adsorptive gas separation process according to claim 1, wherein said fuel combustor comprises at least one of a gaseous fuel, liquid fuel and solid fuel fired combustor.
 4. The integrated adsorptive gas separation process according to claim 1, wherein said fuel combustor comprises at least one of: a combined cycle gas turbine combustor; a gas turbine combustor; a coal-fired thermal combustor; a steam generator or boiler combustor; and a process heater combustor.
 5. The integrated adsorptive gas separation process according to claim 1, wherein said combustion gas mixture comprises about 12% carbon dioxide, and wherein said first portion of said first component comprises about 4% of said combustion gas mixture, and said second portion of said first component recycled to said combustor comprises about 8% of said combustion gas mixture.
 6. The integrated adsorptive gas separation process according to claim 1, wherein said first product gas is substantially free of said first component, and said desorbed second product gas consists substantially of said first component.
 7. The integrated adsorptive gas separation process according to claim 1, wherein said adsorptive gas separation system comprises at least one parallel passage adsorbent contactor, said parallel passage adsorbent contactor comprising: a plurality of substantially parallel fluid flow passages oriented in a first axial direction between an inlet and an outlet end thereof; and cell walls situated between said fluid flow passages comprising at least one adsorbent material.
 8. The integrated adsorptive gas separation process according to claim 7, wherein said at least one adsorbent contactor additionally comprises a plurality of axially continuous thermally conductive filaments oriented in said first axial direction and in direct contact with said at least one adsorbent material, and said process additionally comprising transferring heat along at least a portion of said thermally conductive filaments in either of said first axial direction or a second axial direction to provide at least a portion of the heat of desorption of said first component during said desorbing step.
 9. The integrated adsorptive gas separation process according to claim 1 wherein said process comprises a thermal swing adsorptive gas separation process, and said adsorbing further comprises adsorbing at least a portion of said first component on said at least one adsorbent material at a first adsorbent material temperature, and said desorbing further comprises desorbing at least a portion of said first component adsorbed on said at least one adsorbent material by heating said adsorbent material at a second adsorbent material temperature.
 10. The integrated adsorptive gas separation process according to claim 1 wherein said process comprises a thermal swing adsorptive gas separation process and wherein said desorbing additionally comprises heating said at least one adsorbent material using a heated process fluid admitted into said adsorptive gas separation system, wherein said heated process fluid comprises at least one of: steam, combustion flue gas, and carbon dioxide.
 11. The integrated adsorptive gas separation process according to claim 1 wherein said process comprises a pressure swing adsorptive gas separation process, and said adsorbing further comprises adsorbing at least a portion of said first component on said at least one adsorbent material at a first pressure, and said desorbing further comprises desorbing at least a portion of said first component adsorbed on said at least one adsorbent material at a second pressure lower than said first pressure.
 12. The integrated adsorptive gas separation process according to claim 1 wherein said process comprises a partial pressure swing adsorptive gas separation process, and said adsorbing further comprises adsorbing at least a portion of said first component on said at least one adsorbent material at a first partial pressure, and said desorbing further comprises desorbing at least a portion of said first component adsorbed on said at least one adsorbent material at a second partial pressure lower than said first partial pressure.
 13. The integrated adsorptive gas separation process according to claim 8, wherein said process comprises a thermal swing adsorptive gas separation process, and wherein said desorbing additionally comprises directly heating at least one said adsorbent material by supplying thermal energy to said thermally conductive filaments to directly heat said cell walls comprising said at least one adsorbent material.
 14. The integrated adsorptive gas separation process according to claim 1, wherein said at least one adsorbent material is selected from the list consisting of: activated carbon adsorbent, amine impregnated adsorbent supports (comprising silica, activated carbon, alumina, zeolite, polymer and ceramic supports), metal salt, metal hydroxide, metal oxide, zeolite, hydrotalcite, silicalite, metal organic framework and zeolitic imadazolate framework adsorbent materials, and combinations thereof.
 15. The integrated adsorptive gas separation process according to claim 1, wherein said admitting, adsorbing, and recovering a first product fluid are conducted at substantially atmospheric pressure, and wherein said desorbing and recovering a desorbed second product fluid steps are conducted at at least one of substantially atmospheric and elevated supra-atmospheric pressures.
 16. The integrated adsorptive gas separation process according to claim 1, wherein said first component enriched conditioning stream is at least one of heated and cooled by contact with an adsorbent contactor of said adsorbent gas separation system during said desorbing of said second portion of said first component adsorbed on said at least one said adsorbent material.
 17. The integrated adsorptive gas separation process according to claim 1, wherein said first component enriched conditioning stream is enriched in carbon dioxide relative to an ambient carbon dioxide concentration in said air and a carbon dioxide concentration of said first product gas depleted in said first component is less than an ambient carbon dioxide concentration of said air.
 18. An integrated adsorptive gas separation system for separating at least a portion of a combustion gas mixture, said combustion gas mixture comprising at least a first component comprising carbon dioxide and a second component, the system comprising: a fuel combustor comprising a combustor air inlet, a combustion chamber and a combustion gas outlet, wherein said combustion gas comprises at least first and second components; an adsorptive gas separator comprising an inlet and an outlet end, wherein said adsorptive gas separator is fluidly connected to said fuel combustor to receive said combustion gas as a feed gas mixture into said inlet end and to adsorb at least a portion of said first component onto at least one adsorbent material comprised in said adsorbent gas separator; and a combustion gas recycle fluid conduit which is fluidly connected to said adsorptive gas separator and to said combustor air inlet, and adapted to receive a desorbed combustion recycle gas comprising at least a portion of said first component adsorbed on said adsorbent material, and to return said desorbed combustion recycle gas to said combustor air inlet.
 19. The integrated adsorptive gas separation system according to claim 18, wherein said adsorptive gas separator additionally comprises a plurality of axially continuous thermally conductive filaments oriented in said axial direction and in direct contact with said at least one adsorbent material and wherein said at least one adsorbent material is selected from the list consisting of: activated carbon adsorbent, amine impregnated adsorbent supports (comprising silica, activated carbon, alumina, zeolite, polymer and ceramic supports), metal salt, metal hydroxide, metal oxide, zeolite, hydrotalcite, silicalite, metal organic framework and zeolitic imadazolate framework adsorbent materials, and combinations thereof.
 20. The integrated adsorptive gas separation system according to claim 18, wherein said fuel combustor comprises at least one of: a combined cycle gas turbine combustor; a gas turbine combustor; a coal-fired thermal combustor; a steam generator or boiler combustor; and a process heater combustor. 